CN210481144U - Sewage treatment device for synchronously realizing sludge in-situ reduction and nitrogen and phosphorus removal - Google Patents
Sewage treatment device for synchronously realizing sludge in-situ reduction and nitrogen and phosphorus removal Download PDFInfo
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Abstract
The utility model relates to a synchronous realization mud normal position decrement and nitrogen and phosphorus removal's sewage treatment plant, complete equipment include along sludge reduction pond, sludge settling tank, coagulating sedimentation tank, ammonia nitrogen adsorption component, aeration tank and the solid-liquid separation unit that sewage treatment direction arranged in proper order, sludge settling tank's surplus sludge outlet still connects through mud return line one the aeration tank, solid-liquid separation unit's surplus sludge outlet still connects through mud return line two sludge reduction pond. Compared with the prior art, the process of the utility model can realize the obvious sludge reduction on the premise that the effluent quality meets the GB18918-2002 first-level A and even the IV-class standard of surface water.
Description
Technical Field
The utility model belongs to the technical field of sewage treatment, a realize sewage treatment plant of mud normal position decrement and nitrogen and phosphorus removal in step is related to.
Background
As the most widely applied sewage treatment technology at present, the activated sludge process treats more than 90 percent of urban sewage and about 50 percent of industrial wastewater in the world. With the rising of sewage treatment rate and the stricter of environmental regulations, the treatment and disposal of excess sludge become the main factors which beset the further development of the activated sludge process, and the investment and operation cost thereof account for about 25-65% of the whole sewage treatment plant. Moreover, the problems of site selection and public support are encountered in both landfill and incineration, and the problem of secondary pollution is also existed. Therefore, how to solve the problem of sludge outlet becomes a major environmental problem to be solved urgently in the urban development process in China, and is also a focus of attention of the world environmental protection industry at present. Compared with the treatment and disposal technology, the method for realizing the in-situ sludge reduction in the sewage treatment process is the best method for solving the problem of excess sludge. Among them, the anaerobic side-flow reactor installed in the sludge return line has the advantages of low operation cost, small influence on microorganisms and the like, and is one of the most possible in-situ reduction processes applied in sewage treatment plants. The process keeps a part of sludge in an anaerobic environment for a certain time after passing through the side flow reactor unit, so that the lower sludge yield is realized, and the settling property of the sludge and the effluent quality are not influenced. Sludge reduction is mainly based on four reduction mechanisms: lysis recessive growth, energy uncoupling metabolism, microbial predation and sludge attenuation.
Among various sludge reduction processes, the OSA process in which a side flow reactor (SSR) is provided on a sludge return line has advantages of simple process, low operation cost, large treatment scale, and the like, and is considered to be the process most likely to be put to practical use. The process is proved to be capable of realizing sludge reduction and improving the sludge settling performance on the premise of not influencing the effluent quality. However, the reaction time required for effective SSR abatement is relatively long, with a minimum Hydraulic Retention Time (HRT) of 6-7 h. For example, the HRT ratio between SSR and mainstream biological treatment systems in Levico wastewater treatment plants in Italy, where ASSR-AO was used throughout the plant, was 0.47. Too long HRT will limit the promotion and application of ASSR, and how to accelerate sludge reduction and reduce occupied area through microbial physiological and ecological regulation is the key to improve the technical competitiveness of the ASSR.
Researches show that SSR insertion does not influence or even improve the sludge settling performance. However, when the sludge generation rate is not matched with the reduction rate, the SSR causes the problem that the solid-liquid separation capacity of the secondary sedimentation tank is insufficient, and the effluent Suspended Solids (SS) are higher. As in the OSA pilot experiments conducted by Comma et al (Bioresource Technology,2013,129: 229-. The sludge reduction process needs to solve the problem of stable standard reaching of the effluent SS and also needs to consider the deterioration of the effluent dephosphorization effect caused by long-sludge-age running. This problem is prevalent in the OSA process currently being studied and reported.
In order to solve the problems, the SSR pool can be inserted into an intermediate sedimentation tank, and the effluent of the SSR pool enters the sedimentation tank for solid-liquid separation so as to effectively buffer the sludge floating problem caused by sludge accumulation. In the SSR pool sludge reduction process, the hydrolysis of particles and the lysis of microorganisms release ammonia nitrogen, and for low-carbon-nitrogen-ratio domestic sewage, the shortage of carbon sources easily causes the excessive nitrogen and phosphorus in the effluent. Therefore, the development of the coupling of the sludge reduction process and the denitrification unit of the double-sludge system has very important significance for improving the sludge reduction efficiency and maintaining the effluent quality to be stable and up to the standard.
SUMMERY OF THE UTILITY MODEL
The utility model aims to overcome the defects of the prior art and provide a sewage treatment device and a process for synchronously realizing sludge in-situ reduction and nitrogen and phosphorus removal. Aiming at the problems that the effluent suspended matters of the sludge sidestream in-situ reduction system are easy to exceed the standard, the nitrogen and phosphorus removal efficiency of the sewage with low carbon-nitrogen ratio is not high, and the like, a brand-new sludge reduction process technology is provided through the coupling of physicochemical and biochemical technologies. The process of the utility model can realize the obvious sludge reduction on the premise that the effluent quality meets the GB18918-2002 first-level A or even surface water IV standard.
The purpose of the utility model can be realized through the following technical scheme:
one of the technical schemes of the utility model lies in providing a realize sewage treatment plant of mud normal position decrement and nitrogen and phosphorus removal in step, include sludge decrement pond, sludge settling tank, coagulating sedimentation tank, ammonia nitrogen adsorption component, aeration tank and the solid-liquid separation unit that arrange in proper order along the sewage treatment direction, sludge settling tank's excess sludge outlet still connects through sludge return line one the aeration tank, solid-liquid separation unit's excess sludge outlet still connects through sludge return line two sludge decrement pond.
Furthermore, the adopted sludge reduction tank can be switched into anaerobic, anoxic and micro-aerobic operation modes according to working conditions, and can be further switched into a full-mixing type anaerobic reactor, an upflow type anaerobic sludge bed, a sludge expansion bed and other modes according to different anaerobic modes, and methane produced by sludge is recovered. Wherein, the fully-mixed anaerobic reactor, the upflow anaerobic sludge blanket and the sludge expansion blanket are all common structures in the field, and the structures are as follows:
a full-mixing type anaerobic reactor: the concrete structure is a closed tank body and a stirring device. The wastewater can be completely mixed with anaerobic sludge and anaerobically digested to produce methane. After the sewage to be treated enters the full-mixing type anaerobic reactor, all anaerobic sludge is quickly mixed by the stirring device, and anaerobic digestion reaction is carried out under the action of anaerobic microorganisms in the sludge, so that the concentration of the anaerobic sludge is always kept in a relatively low state, and finally sludge reduction is realized.
Upflow anaerobic sludge blanket: the upflow anaerobic sludge blanket is mainly composed of a water distribution system at the bottom, an anaerobic reaction zone at the lower part and a gas-liquid-solid three-phase separator at the upper part. The sewage to be treated enters the reactor, is mixed with anaerobic sludge in the lower anaerobic zone to carry out reactions such as anaerobic digestion and sludge reduction, and the generated gas such as methane is discharged from a triangular area at the bottom of the herringbone baffle plate of the three-phase separator. And (3) discharging the effluent, residual gas and sludge from the top of the mixed sludge under the action of natural sedimentation and a three-phase separator, and performing the next biological treatment.
Sludge expansion bed: the sludge expanded bed has great similarity with an up-flow anaerobic sludge bed in terms of structural form and sludge form. But the sludge expansion bed is additionally provided with a treated water circulation system, the flow rate of liquid in the reactor is improved, the sludge bed in the reactor is expanded, and the full contact between the sewage to be treated and anaerobic sludge can be ensured.
Furthermore, a dephosphorization dosing tank is arranged on a connecting pipeline between the sludge sedimentation tank and the coagulation sedimentation tank. Furthermore, the phosphorus removal agent in the phosphorus removal medicine adding box can be selected from compounds added with calcium, aluminum or iron, such as lime, alum, ferric trichloride and the like.
Further, the ammonia nitrogen adsorption component comprises at least one group of ammonia nitrogen adsorption columns, and a water inlet and a water outlet of each ammonia nitrogen adsorption column are respectively connected with the coagulating sedimentation tank and the aeration tank.
Furthermore, the ammonia nitrogen adsorption column comprises a water inlet, a water outlet and an ammonia nitrogen adsorption material filled between the water inlet and the water outlet, and the ammonia nitrogen adsorption material which can be utilized comprises a molecular sieve, activated carbon, ceramsite, zeolite, ion exchange resin and the like.
Preferably, two or more sets of ammonia nitrogen adsorption columns are arranged, so that a single set of ammonia nitrogen adsorption column is switched to a regeneration stage after adsorption penetration, and the inflow is switched to the other set for continuous operation.
Furthermore, a regeneration liquid box connected with the ammonia nitrogen adsorption column through a regeneration pipeline is arranged at the water inlet of the ammonia nitrogen adsorption column, and a regeneration waste liquid discharge pipeline is arranged at the water outlet of the ammonia nitrogen adsorption column.
Further, the solid-liquid separation unit is a secondary sedimentation tank, supernatant of the secondary sedimentation tank is discharged through a water outlet pipeline, and residual sludge at the bottom is respectively returned and connected with the sludge reduction tank and the aeration tank through the sludge return pipeline II.
Furthermore, the solid-liquid separation unit is a membrane separation assembly arranged in an aeration tank, a sludge outlet is processed at the bottom of the aeration tank and is used as a residual sludge outlet of the solid-liquid separation unit, and a second sludge return pipeline is arranged and is respectively connected with the sludge outlet and the sludge reduction tank. The membrane separation module can adopt membrane separation equipment which is commonly used in the field and can realize the filtration of the sewage.
The sewage to be treated enters a sludge reduction tank, is uniformly mixed with the returned residual sludge, and is kept in an anaerobic environment for a certain time. Sludge is reduced in the sludge reduction tank based on four reduction mechanisms of lysis recessive growth, energy uncoupling metabolism, microbial predation and sludge attenuation. And the reactions of denitrification reaction, anaerobic phosphorus release and the like occur simultaneously. And the sewage treated by the sludge reduction tank enters a sludge sedimentation tank for sludge-water separation. Part of the sludge flows back to the aerobic tank to supplement the sludge concentration in the system, and the other part of the sludge is discharged as residual sludge. The separated sewage contains higher concentration of total phosphorus because of the reactions such as anaerobic phosphorus release and the like in the sludge reduction tank. The sewage gets into and carries out the coagulating sedimentation in the coagulating sedimentation pond and handles, gets rid of most total phosphorus and suspended solid, makes into water and is unlikely to block up ammonia nitrogen adsorption component. The influent water is subjected to ion adsorption in the ammonia nitrogen adsorption component to remove most ammonia nitrogen. The effluent with low phosphorus content and low ammonia nitrogen enters an aeration tank, is beneficial to the combined action of aerobic microorganisms such as phosphorus-accumulating bacteria glycan bacteria and the like, removes soluble organic matters, and finally realizes the standard-reaching discharge of sewage treatment
The second technical scheme of the utility model lies in providing a sewage treatment process of synchronous realization mud normal position decrement and nitrogen and phosphorus removal, including following step:
(1) after the sewage to be treated is sent into a sludge reduction tank for treatment, the treated sewage is discharged into a sludge sedimentation tank for primary sedimentation, the obtained supernatant is added with a phosphorus removal medicament and then enters a coagulation sedimentation tank for sedimentation treatment, and part of the obtained residual sludge is directly sent into an aeration tank in the step (2);
(2) the dephosphorization sewage obtained after the coagulation sedimentation in the coagulation sedimentation tank enters an ammonia nitrogen adsorption component, is subjected to ammonia nitrogen adsorption treatment and then is sent into an aeration tank for aeration treatment;
(3) and treating the sewage after the aeration treatment in the aeration tank by a solid-liquid separation unit, discharging the obtained clear liquid as effluent, and returning the obtained residual sludge to the aeration tank and the sludge reduction tank respectively.
Further, in the step (1), the treatment process of the sewage to be treated in the sludge reduction tank is specifically as follows: and (3) arranging stirring equipment in the sludge reduction tank, uniformly mixing the sewage to be treated and the returned sludge, wherein the sludge concentration is 4-10 g SS/L, the oxygen concentration is about 0.2mg/L, and the hydraulic retention time is 4-10 h. In the sludge reduction tank, through the reactions of return sludge denitrification, sludge anaerobic phosphorus release, sludge reduction and the like, when sewage enters the sedimentation tank, the concentration of pollutants such as ammonia nitrogen, total phosphorus and the like may be higher than that of the sewage to be treated, and the concentration of pollutants such as chemical oxygen demand and the like may be lower than that of the sewage to be treated.
Further, in the step (1), the phosphorus removal agent is a compound of calcium, aluminum or iron, the addition amount of the phosphorus removal agent is 5-1500 mg/g SS, and the phosphorus removal agent is adjusted according to actual conditions. Too low dosage can cause too high concentration of total phosphorus in effluent, and too high dosage can cause reduction of sludge activity and inhibit nitrification rate to a certain extent;
in the step (2), the ammonia nitrogen adsorption treatment time is 0.2-4 h, and the ammonia nitrogen adsorption treatment time is adjusted according to actual conditions. Too low an adsorption time may result in too high a total nitrogen in the effluent, and too long an adsorption time may increase the cost;
in the step (3), the time of aeration treatment is 0.5-10 h, the aeration rate meets the requirement that the oxygen concentration in the water body of the aeration tank is 0.8-8 mg/L, and the aeration rate is adjusted according to actual conditions. Lower aeration rates may result in effluent contaminant concentrations that fail to meet standards.
Furthermore, after the ammonia nitrogen adsorption component runs for a set time, regeneration is realized by introducing a regeneration liquid from a water inlet of the ammonia nitrogen adsorption component for soaking treatment. The salt in the regeneration liquid can be selected from calcium salt, potassium salt, magnesium salt, zinc salt, ferric salt, aluminum salt and sodium salt, the concentration of the salt is 4-90 g/L, and the salt is adjusted according to actual conditions. Lower concentrations may result in incomplete regeneration of the adsorbent element, while higher concentrations may damage the adsorbent material, reduce denitrification efficiency, and increase costs.
Compared with the prior art, the utility model has the advantages of it is following:
(1) the coupling of the high-efficiency physicochemical nitrogen and phosphorus removal technology and the biological treatment technology greatly shortens the reaction time and reduces the occupied land. Traditional nitrogen and phosphorus removal technology needs the water conservancy dwell time that reaches 20h to realize that one-level A is up to standard because the setting of oxygen deficiency, anaerobism, good oxygen unit the utility model discloses in because chemical phosphorus removal and ammonia nitrogen adsorption rate all can be accomplished fast, the steerable 8 hours that are less than of total hydraulic power dwell time of reactor, reduced process systems' area by a wide margin.
(2) The combination of efficient pollutant removal and sludge reduction technology realizes the purpose of greatly reducing the sludge yield while the sewage is treated to reach the standard, and the sludge yield is only 10-20% of that of the traditional technology.
(3) The process is flexible in design and is beneficial to resource utilization of substances. The sludge reduction tank can be switched to an anaerobic mode for operation, and organic matters in the sewage can be converted into methane for recycling while sludge reduction is carried out; due to the solid-liquid pre-separation of the sludge reduction tank, the precipitate with higher phosphorus content can be obtained by removing phosphorus in the coagulating sedimentation tank, and the recycling of phosphorus resources is facilitated.
Drawings
FIG. 1 is a schematic view of a process flow for synchronously realizing efficient sludge in-situ reduction and nitrogen and phosphorus removal;
FIG. 2 is a schematic view of another process flow for synchronously realizing efficient sludge in-situ reduction and nitrogen and phosphorus removal;
the notation in the figure is:
1 is a water inlet pump; 2 is a sludge reduction tank; 3 is a sludge sedimentation tank; 4 is a coagulating sedimentation tank; 5 is an ammonia nitrogen adsorption column; 6 is an aeration tank; 7 is a secondary sedimentation tank; 8 is a water outlet pump; 9 is a second sludge reflux pump; 10 is a first dredge pump; 11 is a second sludge discharge pump; 12 is a first ammonia nitrogen adsorption column water inlet pump; 13 is a second ammonia nitrogen adsorption column water inlet pump; 14 is a water outlet pump of the first ammonia nitrogen adsorption column; 15 is a water outlet pump of the second ammonia nitrogen adsorption column; 16 is a regenerated liquid pump; 17 is a regeneration waste liquid discharge pump; 18 is a first sludge reflux pump; 19 is a dephosphorization dosing pump; 20 is a third sludge reflux pump; and 21 is a membrane separation module.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings and specific embodiments. The embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.
One of the technical schemes of the utility model lies in providing a realize sewage treatment plant of mud normal position decrement and nitrogen and phosphorus removal in step, include the mud decrement pond 2, the sludge settling pond 3, the coagulating sedimentation pond 4, ammonia nitrogen adsorption component, aeration tank 6 and the solid-liquid separation unit that arrange in proper order along the sewage treatment direction, the excess sludge outlet of sludge settling pond 3 still passes through sludge return line one (can set up first sludge reflux pump 18 above that) and connects aeration tank 6, the excess sludge outlet of solid-liquid separation unit still passes through sludge return line two and connects sludge decrement pond 2.
The utility model discloses an among the concrete embodiment, the mud decrement pond 2 that adopts can select to be anaerobism, oxygen deficiency and little oxygen operational mode according to operating condition's difference, can further select operational mode such as full mixed formula anaerobic reactor, upflow anaerobic sludge bed, mud expanded bed according to the anaerobism mode operation to methane to mud is produced retrieves. Wherein, the full-mixing type anaerobic reactor: the concrete structure is a closed tank body and a stirring device. The wastewater can be completely mixed with anaerobic sludge and anaerobically digested to produce methane. After the sewage to be treated enters the reactor, all anaerobic sludge is quickly mixed by the stirring device, anaerobic digestion reaction is carried out under the action of anaerobic microorganisms in the sludge, so that the concentration of the anaerobic sludge is always kept in a relatively low state, and finally sludge reduction is realized.
Upflow anaerobic sludge blanket: the upflow anaerobic sludge blanket is mainly composed of a water distribution system at the bottom, an anaerobic reaction zone at the lower part and a gas-liquid-solid three-phase separator at the upper part. The sewage to be treated enters the reactor, is mixed with anaerobic sludge in the lower anaerobic zone to carry out reactions such as anaerobic digestion and sludge reduction, and the generated gas such as methane is discharged from a triangular area at the bottom of the herringbone baffle plate of the three-phase separator. And (3) discharging the effluent, residual gas and sludge from the top of the mixed sludge under the action of natural sedimentation and a three-phase separator, and performing the next biological treatment.
Sludge expansion bed: the sludge expanded bed has great similarity with an up-flow anaerobic sludge bed in terms of structural form and sludge form. But the sludge expansion bed is additionally provided with a treated water circulation system, the flow rate of liquid in the reactor is improved, the sludge bed in the reactor is expanded, and the full contact between the sewage to be treated and anaerobic sludge can be ensured.
In a specific embodiment of the utility model, a dephosphorization dosing box is further arranged on the connecting pipeline between the sludge settling tank 3 and the coagulating sedimentation tank 4. Furthermore, the phosphorus removal agent in the phosphorus removal medicine adding box can be selected from compounds added with calcium, aluminum or iron, such as lime, alum, ferric trichloride and the like. The phosphorus removal dosing tank can be connected to this connection line via a line with a phosphorus removal dosing pump 19.
The utility model discloses an in a specific embodiment, ammonia nitrogen adsorption component includes at least a set of ammonia nitrogen adsorption column 5, the water inlet of ammonia nitrogen adsorption column 5 (can set up 5 intake pumps of ammonia nitrogen adsorption column) is connected respectively with the delivery port (can set up 5 water pumps of ammonia nitrogen adsorption column) coagulating sedimentation tank 4 and aeration tank 6.
Furthermore, the ammonia nitrogen adsorption column 5 comprises a water inlet, a water outlet and an ammonia nitrogen adsorption material filled between the water inlet and the water outlet, and the ammonia nitrogen adsorption material which can be utilized comprises a molecular sieve, activated carbon, ceramsite, zeolite, ion exchange resin and the like.
Preferably, two or more sets of ammonia nitrogen adsorption columns 5 are arranged, so that a single set of ammonia nitrogen adsorption column 5 is switched to a regeneration stage after adsorption penetration, and the inlet water is switched to the other set for continuous operation.
Furthermore, a regeneration liquid tank connected with the ammonia nitrogen adsorption column 5 through a regeneration pipeline is arranged at the water inlet, a regeneration waste liquid discharge pipeline is additionally arranged at the water outlet of the ammonia nitrogen adsorption column 5, and a regeneration waste liquid discharge pump can be arranged on the regeneration waste liquid discharge pipeline.
In a specific embodiment of the present invention, the solid-liquid separation unit is a secondary sedimentation tank 7, the supernatant of the secondary sedimentation tank 7 is discharged through a water outlet pipeline, and the residual sludge at the bottom is passed through a sludge return pipeline two for respectively returning and connecting the sludge reduction tank 2 and the aeration tank 6. More specifically, the sludge return line is bifurcated, and one of the sludge return lines is returned to the aeration tank 6 by the third sludge return pump 20. The other fork opening returns to the sludge reduction tank 2 through a second sludge reflux pump 9.
In a specific embodiment of the present invention, the solid-liquid separation unit is a membrane separation module 21 disposed in the aeration tank 6, and a sludge outlet is processed at the bottom of the aeration tank 6 as the residual sludge outlet of the solid-liquid separation unit, and the sludge return line two is connected to the sludge outlet and the sludge reduction tank 2, respectively. The membrane separation module 21 may employ a membrane separation device commonly used in the art to filter the contaminated water.
The sewage to be treated enters a sludge reduction tank, is uniformly mixed with the returned residual sludge, and is kept in an anaerobic environment for a certain time. Sludge is reduced in the sludge reduction tank based on four reduction mechanisms of lysis recessive growth, energy uncoupling metabolism, microbial predation and sludge attenuation. And the reactions of denitrification reaction, anaerobic phosphorus release and the like occur simultaneously. And the sewage treated by the sludge reduction tank enters a sludge sedimentation tank for sludge-water separation. Part of the sludge flows back to the aerobic tank to supplement the sludge concentration in the system, and the other part of the sludge is discharged as residual sludge. The separated sewage contains higher concentration of total phosphorus because of the reactions such as anaerobic phosphorus release and the like in the sludge reduction tank. The sewage gets into and carries out the coagulating sedimentation in the coagulating sedimentation pond and handles, gets rid of most total phosphorus and suspended solid, makes into water and is unlikely to block up ammonia nitrogen adsorption component. The influent water is subjected to ion adsorption in the ammonia nitrogen adsorption component to remove most ammonia nitrogen. And the effluent with low phosphorus content and low ammonia nitrogen enters an aeration tank, and the soluble organic matters are removed under the combined action of aerobic microorganisms such as the polyphosphate accumulating bacteria and the like, so that the standard-reaching discharge of sewage treatment is finally realized.
The second technical scheme of the utility model lies in providing a sewage treatment process of synchronous realization mud normal position decrement and nitrogen and phosphorus removal, including following step:
(1) after the sewage to be treated is sent into the sludge reduction tank 2 for treatment, the obtained treated sewage is discharged into the sludge sedimentation tank 3 for primary sedimentation, the obtained supernatant is added with a phosphorus removal medicament and then enters the coagulating sedimentation tank 4 for sedimentation treatment, and part of the obtained residual sludge is directly sent into the aeration tank 6 in the step (2);
(2) the dephosphorization wastewater obtained after the coagulation sedimentation in the coagulation sedimentation tank 4 enters an ammonia nitrogen adsorption component, is subjected to ammonia nitrogen adsorption treatment and then is sent into an aeration tank 6 for aeration treatment;
(3) the sewage after the aeration treatment in the aeration tank 6 is treated by a solid-liquid separation unit, the obtained clear liquid is discharged as effluent, and the obtained excess sludge is respectively returned to the aeration tank 6 and the sludge reduction tank 2.
In a specific embodiment of the present invention, in step (1), the treatment process of the sewage to be treated in the sludge reduction tank 2 specifically comprises: a stirrer is arranged in the sludge reduction tank, the sewage to be treated and the returned sludge are uniformly mixed, the sludge concentration is 4-10 g SS/L, the oxygen concentration is about 0.2mg/L, and the hydraulic retention time is 4-10 h. In the sludge reduction tank, through the reactions of return sludge denitrification, sludge anaerobic phosphorus release, sludge reduction and the like, when sewage enters the sedimentation tank, the concentration of pollutants such as ammonia nitrogen, total phosphorus and the like may be higher than that of the sewage to be treated, and the concentration of pollutants such as chemical oxygen demand and the like may be lower than that of the sewage to be treated.
In a specific embodiment of the present invention, in the step (1), the phosphorus removal agent is a compound of calcium, aluminum or iron, and the addition amount thereof is 5 to 1500mg/g SS.
The utility model discloses an in a specific embodiment, in step (2), the time of ammonia nitrogen adsorption treatment is (0.2 ~ 4 h) to adjust according to actual conditions.
In a specific embodiment of the present invention, in step (3), the time of the aeration treatment is 0.5 to 10 hours, and the aeration amount satisfies that the oxygen concentration in the water body of the aeration tank 6 is 0.8 to 8mg/L, and is adjusted according to the actual situation.
The utility model discloses an in a specific embodiment, after ammonia nitrogen adsorption component operation settlement time, through letting in regeneration liquid soaking treatment back from its water inlet, realize the regeneration.
The above embodiments may be implemented individually, or in any combination of two or more.
The above embodiments will be further described with reference to specific examples.
Example 1:
as shown in fig. 1, in the sewage treatment process for synchronously implementing high-efficiency sludge in-situ reduction and nitrogen and phosphorus removal in this embodiment, the grid inlet water enters a sludge reduction tank 2 (anaerobic mode) through a water inlet pump 1, and after the grid inlet water reacts with 100% excess sludge returned by a second sludge reflux pump 9 for 6.7 hours, the grid inlet water enters a sludge sedimentation tank 3 for sedimentation of sludge for 3 hours, the supernatant is phosphorus removed by adding ferric trichloride through a phosphorus removal dosing pump 19 and then enters a coagulation sedimentation tank 4 for sedimentation, and the sludge discharge period of the coagulation sedimentation tank 4 is 3 hours. The dephosphorization wastewater is pumped into the ammonia nitrogen adsorption column 4 through a first ammonia nitrogen adsorption column water inlet pump 12 and a second ammonia nitrogen adsorption column water inlet pump 13, ammonia nitrogen is adsorbed for 15min, the wastewater flows out of the ammonia nitrogen adsorption column 4 through a first ammonia nitrogen adsorption column water outlet pump 14 and a second ammonia nitrogen adsorption column water outlet pump 15, then enters an aeration tank 6 for biological treatment for 6h, the aeration tank 6 receives 100% of sludge from a sludge sedimentation tank 3 through a first sludge reflux pump 18, the sludge and activated sludge added in advance are subjected to biological treatment, the wastewater enters a secondary sedimentation tank 7 for sedimentation for 1h, and the effluent is discharged through a water outlet pump 8.
The sludge is subjected to anaerobic reaction and sludge reduction in the sludge reduction tank 2, most of ammonia nitrogen sewage is removed by the ammonia nitrogen adsorption column 5, the rest low ammonia nitrogen wastewater enters the aeration tank 6 to undergo nitration reaction and the like to remove organic matters, and the sludge with 100% of water inlet flow flows back to the sludge reduction tank 1. After the ammonia nitrogen adsorption column 5 runs for 24 hours for adsorption saturation, the regenerated liquid is pumped into the regenerated liquid tank from the regenerated liquid tank through the regenerated liquid pump 16 for regeneration for 4 hours, and the regenerated waste liquid is pumped out by the regenerated waste liquid discharge pump 17. After regeneration for a certain number of times, the regeneration liquid can be subjected to calcium removal treatment, and the treated regeneration liquid can be recycled.
The operation is continued for 100 days according to the process mode. The average concentration of soluble COD, ammonia nitrogen, total nitrogen and total phosphorus in the inlet water is 280.5, 60.2, 75.1 and 15.4 mg/L. After the treatment by the process provided by the utility model, the pH value of the reactor is 6.5-7.5, and the average concentration of effluent COD, ammonia nitrogen, total nitrogen and total phosphorus is 15.2, 0.5, 3.4 and 0.3mg/L respectively. The sludge yield is reduced by 75 percent compared with the same period in the last year.
The ammonia nitrogen adsorption column of this embodiment adopts the zeolite column.
Example 2
High ammonia nitrogen wastewater with coarse floaters and suspended matters intercepted by a grid in a certain sewage plant enters a sludge reduction tank 2 with the HRT of 6h through a water inlet pump 1 and is fully mixed and contacted with return sludge. Then enters a sludge sedimentation tank 3 with HRT of 2h for sludge-water separation. And (3) removing phosphorus from the separated supernatant, entering an ammonia nitrogen adsorption column 4 with HRT of 0.5h to remove most of ammonia nitrogen, and switching to a regeneration stage after a single ammonia nitrogen adsorption column 4 continuously runs for 12h and penetrates through the column, wherein the inflow water is switched to another adsorption column for continuous operation. When the ammonia nitrogen adsorption column 4 regenerates, the regeneration liquid pump 16 pumps regeneration liquid into the ammonia nitrogen adsorption column, desorbs and regenerates the adsorption material, and converts the desorbed ammonia nitrogen into nitrogen. Wherein the concentration of the composite regeneration liquid is 40g/L, and the regeneration soaking time is 4 h. Then enters an aeration tank 5 with the HRT of 6.5 h. At the moment, the ammonia nitrogen of the inlet water is low, and the nitrate nitrogen is subjected to denitrification in the sludge reduction tank 2 by utilizing the inlet water carbon source. Most of ammonia nitrogen is adsorbed in the ammonia nitrogen adsorption column 4, so that a carbon source in the system can be fully utilized by the phosphorus accumulating bacteria, and the total phosphorus in the effluent reaches the standard. Finally, the effluent is discharged through the membrane module.
Through the continuous 6-month operation of the mode, the average concentration of soluble COD, ammonia nitrogen, total nitrogen and total phosphorus in the inlet water is 180.5, 100.2, 150.3 and 10.0 mg/L. After the treatment by the process provided by the utility model, the pH value of the reactor is 6.5-7.5, and the average concentration of effluent COD, ammonia nitrogen, total nitrogen and total phosphorus is 10.1, 5.0, 7.0 and 0.8mg/L respectively. The sludge yield is reduced by 70 percent compared with the same period of the last year.
Comparative example 1
Compared with the embodiment 1, the ammonia nitrogen adsorption component is mostly the same except that the ammonia nitrogen adsorption component is removed in the embodiment. At the moment, after the ammonia nitrogen adsorption component in the figure 1 is removed, the water enters the sludge reduction tank 2 (anaerobic mode) through the grid inlet pump 1, reacts with the excess sludge with 100% inlet water flow returned by the second sludge reflux pump 9 for 6.7 hours, enters the sludge sedimentation tank 3 for sedimentation of sludge for 3 hours, the supernatant enters the coagulation sedimentation tank 4 for sedimentation after phosphorus removal by the phosphorus removal dosing pump 19 and iron trichloride, and the sludge discharge period of the coagulation sedimentation tank 4 is 3 hours. The dephosphorization wastewater enters an aeration tank 6 for biological treatment for 6h, the aeration tank 6 receives 100% of sludge from a sludge sedimentation tank 3 by a first sludge reflux pump 18, the sludge and activated sludge added in advance are subjected to biological treatment, the sludge enters a secondary sedimentation tank 7 for sedimentation for 1h, and effluent is discharged by a water outlet pump 8.
The sludge is subjected to anaerobic reaction and sludge reduction in the sludge reduction tank 2, a large amount of ammonia nitrogen and soluble organic matters are released by sludge reduction actions such as sludge cell dissolution and the like in the sludge reduction tank, then the sewage enters the aeration tank 6 to be subjected to nitration reaction and the like to remove the organic matters, and the sludge with 100 percent of water inlet flow flows back to the sludge reduction tank 1. Because a large amount of nitrate is generated in the nitration process, the utilization of the carbon source by the microorganism is prior to the biological phosphorus removal in the denitrification process, so that the total phosphorus in the effluent cannot reach the standard.
The operation is continued for 100 days according to the process mode. The average concentration of soluble COD, ammonia nitrogen, total nitrogen and total phosphorus in the inlet water is 260.4, 40.5, 60.3 and 20.1 mg/L. After the treatment by the process, the pH value of the reactor is 6.5-7.5, and the average concentrations of COD, ammonia nitrogen, total nitrogen and total phosphorus in the effluent are respectively 19.6, 8.5, 14.6 and 0.7 mg/L. The sludge yield is reduced by 25 percent compared with the same period in the last year.
The embodiments described above are intended to facilitate the understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention according to the disclosure of the present invention.
Claims (6)
1. The sewage treatment device is characterized by comprising a sludge reduction tank, a sludge sedimentation tank, a coagulating sedimentation tank, an ammonia nitrogen adsorption component, an aeration tank and a solid-liquid separation unit which are sequentially arranged along the sewage treatment direction, wherein the residual sludge outlet of the sludge sedimentation tank is also connected with the aeration tank through a sludge return pipeline I, and the residual sludge outlet of the solid-liquid separation unit is also connected with the sludge reduction tank through a sludge return pipeline II.
2. The sewage treatment plant for synchronously realizing the in-situ sludge reduction, the nitrogen removal and the phosphorus removal as claimed in claim 1, wherein a phosphorus removal dosing tank is further arranged on a connecting pipeline between the sludge sedimentation tank and the coagulation sedimentation tank.
3. The sewage treatment device for synchronously realizing in-situ sludge reduction, nitrogen and phosphorus removal according to claim 1, wherein the ammonia nitrogen adsorption component comprises at least one group of ammonia nitrogen adsorption columns, and a water inlet and a water outlet of each ammonia nitrogen adsorption column are respectively connected with the coagulating sedimentation tank and the aeration tank.
4. The sewage treatment plant for synchronously realizing in-situ sludge reduction, nitrogen and phosphorus removal according to claim 3, wherein a regeneration liquid tank connected with the ammonia nitrogen adsorption column through a regeneration pipeline is further arranged at the water inlet of the ammonia nitrogen adsorption column, and a regeneration waste liquid discharge pipeline is further arranged at the water outlet of the ammonia nitrogen adsorption column.
5. The sewage treatment plant according to claim 1, wherein the solid-liquid separation unit is a secondary sedimentation tank, the supernatant of the secondary sedimentation tank is discharged through a water outlet pipeline, and the residual sludge at the bottom is returned through the sludge return pipeline II to connect the sludge reduction tank and the aeration tank respectively.
6. The sewage treatment plant according to claim 1, wherein the solid-liquid separation unit is a membrane separation module disposed in an aeration tank, a sludge outlet is formed at the bottom of the aeration tank as a residual sludge outlet of the solid-liquid separation unit, and the sludge return line II is disposed to connect the sludge outlet and the sludge reduction tank, respectively.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110342750A (en) * | 2019-07-29 | 2019-10-18 | 上海电力大学 | The synchronous sewage-treatment plant and technique for realizing sludge in-situ decrement and denitrogenation dephosphorizing |
| CN112794581A (en) * | 2021-01-15 | 2021-05-14 | 上海电力大学 | Concentric cylinder type sewage treatment device and process for synchronously realizing sludge in-situ reduction and pollutant removal |
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2019
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110342750A (en) * | 2019-07-29 | 2019-10-18 | 上海电力大学 | The synchronous sewage-treatment plant and technique for realizing sludge in-situ decrement and denitrogenation dephosphorizing |
| CN112794581A (en) * | 2021-01-15 | 2021-05-14 | 上海电力大学 | Concentric cylinder type sewage treatment device and process for synchronously realizing sludge in-situ reduction and pollutant removal |
| CN112794581B (en) * | 2021-01-15 | 2024-04-26 | 上海电力大学 | Concentric cylinder type sewage treatment device and technology for synchronously realizing sludge in-situ reduction and pollutant removal |
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